CN108779405A - Method and apparatus for producing methanation gas - Google Patents
Method and apparatus for producing methanation gas Download PDFInfo
- Publication number
- CN108779405A CN108779405A CN201780017030.5A CN201780017030A CN108779405A CN 108779405 A CN108779405 A CN 108779405A CN 201780017030 A CN201780017030 A CN 201780017030A CN 108779405 A CN108779405 A CN 108779405A
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- China
- Prior art keywords
- steam
- injector
- gas
- methanator
- dry drum
- Prior art date
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- 238000000034 method Methods 0.000 title claims abstract description 44
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims abstract description 46
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 14
- 238000010438 heat treatment Methods 0.000 claims abstract description 11
- 238000004519 manufacturing process Methods 0.000 claims abstract description 9
- 230000015572 biosynthetic process Effects 0.000 claims abstract description 7
- 239000007788 liquid Substances 0.000 claims abstract description 6
- 238000003786 synthesis reaction Methods 0.000 claims abstract description 6
- 238000011144 upstream manufacturing Methods 0.000 claims abstract description 5
- 230000008569 process Effects 0.000 claims description 16
- 239000000571 coke Substances 0.000 claims description 12
- 238000004064 recycling Methods 0.000 claims description 10
- 239000003245 coal Substances 0.000 claims description 7
- 239000002028 Biomass Substances 0.000 claims description 4
- 229920006395 saturated elastomer Polymers 0.000 claims description 4
- 230000008859 change Effects 0.000 claims description 3
- 238000002309 gasification Methods 0.000 claims description 3
- 238000000197 pyrolysis Methods 0.000 claims description 3
- 239000002699 waste material Substances 0.000 claims description 3
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims description 2
- 239000005864 Sulphur Substances 0.000 claims description 2
- 239000007789 gas Substances 0.000 description 40
- 239000000047 product Substances 0.000 description 12
- 238000006243 chemical reaction Methods 0.000 description 11
- 239000004215 Carbon black (E152) Substances 0.000 description 8
- 229930195733 hydrocarbon Natural products 0.000 description 8
- 150000002430 hydrocarbons Chemical class 0.000 description 8
- 238000009835 boiling Methods 0.000 description 6
- 239000012530 fluid Substances 0.000 description 6
- 238000001816 cooling Methods 0.000 description 5
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 4
- 239000003054 catalyst Substances 0.000 description 4
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 3
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 3
- 229910052799 carbon Inorganic materials 0.000 description 3
- 229910002092 carbon dioxide Inorganic materials 0.000 description 3
- 229910052739 hydrogen Inorganic materials 0.000 description 3
- 239000001257 hydrogen Substances 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 2
- LCGLNKUTAGEVQW-UHFFFAOYSA-N Dimethyl ether Chemical compound COC LCGLNKUTAGEVQW-UHFFFAOYSA-N 0.000 description 2
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 2
- 229910000831 Steel Inorganic materials 0.000 description 2
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N Titan oxide Chemical compound O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 description 2
- 230000009471 action Effects 0.000 description 2
- 229910002091 carbon monoxide Inorganic materials 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000000446 fuel Substances 0.000 description 2
- 239000003949 liquefied natural gas Substances 0.000 description 2
- 239000003345 natural gas Substances 0.000 description 2
- 239000000376 reactant Substances 0.000 description 2
- 239000012495 reaction gas Substances 0.000 description 2
- 239000004449 solid propellant Substances 0.000 description 2
- 238000010025 steaming Methods 0.000 description 2
- 239000010959 steel Substances 0.000 description 2
- 150000001335 aliphatic alkanes Chemical class 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 239000003575 carbonaceous material Substances 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000005530 etching Methods 0.000 description 1
- 239000002737 fuel gas Substances 0.000 description 1
- 239000003502 gasoline Substances 0.000 description 1
- XLYOFNOQVPJJNP-ZSJDYOACSA-N heavy water Substances [2H]O[2H] XLYOFNOQVPJJNP-ZSJDYOACSA-N 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 239000004615 ingredient Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 230000001737 promoting effect Effects 0.000 description 1
- 238000005086 pumping Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 230000006641 stabilisation Effects 0.000 description 1
- 238000011105 stabilization Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 230000002195 synergetic effect Effects 0.000 description 1
- 239000004408 titanium dioxide Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
- C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
- C10L3/08—Production of synthetic natural gas
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C1/00—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon
- C07C1/02—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon from oxides of a carbon
- C07C1/04—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon from oxides of a carbon from carbon monoxide with hydrogen
- C07C1/0485—Set-up of reactors or accessories; Multi-step processes
- C07C1/049—Coupling of the reaction and regeneration of the catalyst
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C9/00—Aliphatic saturated hydrocarbons
- C07C9/02—Aliphatic saturated hydrocarbons with one to four carbon atoms
- C07C9/04—Methane
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
- C10L2290/06—Heat exchange, direct or indirect
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
- C10L2290/10—Recycling of a stream within the process or apparatus to reuse elsewhere therein
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
- C10L2290/14—Injection, e.g. in a reactor or a fuel stream during fuel production
- C10L2290/148—Injection, e.g. in a reactor or a fuel stream during fuel production of steam
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
- C10L2290/48—Expanders, e.g. throttles or flash tanks
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Engineering & Computer Science (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Industrial Gases (AREA)
Abstract
A method of for from product gas of the synthesis gas charging production rich in methane, it to include injector to include (a) part for the effluent from methanator being recycled back into the feeding flow of reactor inlet；(b) injector is run with superheated steam, (c) removes liquid water in throttle valve downstream；(d) steam from dry drum is divided into recirculation flow and stream to be output；(e) using at least part of isenthalpic throttling of the steam from dry drum, then steam is reheated with its own in throttle valve upstream, the superheater without technique heating.
Description
The present invention relates to for the method by product of the synthesis gas charging production rich in methane.In addition, the present invention relates to
In the equipment for implementing this method.
The low availability of the gentle fluid fuel of fossil liquid of such as oil and natural gas makes people pay close attention to again can be from wide
General available resource (such as coal, biomass and exhaust gas from coke oven) is synthetically produced the exploitation of the technology of fuel gas.Institute
The gas of generation is well-known to substitute natural gas or synthetic natural gas (SNG), with methane as its main component.
The present invention relates to the methods and apparatus of production methanation gas.Particularly, methanation gas is SNG, and the party
The charging of method is originated from coke oven, is originated from coal, the gasification of biomass and/or waste or from biogas or pyrolysis gas.Preferably, into
Material is coke-stove gas (COG).
Coke is the solid fuel generated by coal by toasting coal in airfree stove.During coke production,
Various volatile coal ingredients are purged and purify, and produce comprising i.e. one or both of carbon dioxide and carbon monoxide
And the exhaust gas of hydrogen and hydrocarbon.This coke oven exhaust gas is rich in energy, and when relatively producing coke with steel mill, is often fired
It burns to generate heat, such as heating coke oven.However, especially when coke in a device be used as solid fuel production without
When other energy requirements, excessive exhaust gas can be obtained.
In methanation, the process of methane is formed in the presence of a catalyst and according to following from oxycarbide and hydrogen
Any of reaction scheme or the two are quickly carried out to balance：
CO+3H2<=>CH4+H2O (1)
CO2+4H2<=>CH4+2H2O (2)
It is not faster critically important to understand which reaction in above-mentioned two reaction, because simultaneously in carbon monoxide and titanium dioxide
There is balance between carbon as follows：
CO+H2O<=>CO2+H2 (3)
Either by reaction (1) or reaction (2) or both, the net reaction of methanogenesis is all high exothermic heat.
Therefore, during by catalyst bed in adiabatic reactor, the temperature of reactants and products will increase.On the other hand,
This raised temperature tends to that balance is made to move towards lower methane concentration.Therefore, only by with such or such
Mode (such as by making to be recycled through cooling product gas) makes reaction gas cooling be increased come limit temperature, could be complete
At or be nearly completed.
Coke oven can be independent device, can also be a part for steel process units.Independent device (commercial coke oven)
There is seldom use or useless to the COG of production.COG mainly locally be used as inferior grade fuel or its only by
Burning.However, since COG is mainly by CH4With synthesis gas (CO+H2) composition, it can be converted into various valuable chemicals
(such as hydrogen, ammonia, methanol and dimethyl ether), SNG, liquefied natural gas (LNG) or synthetic gasoline.
COG can be used for the method by being developed by applicant to produce SNG, and the method includes coming from the first methane
Change reactor and if applicable, is recycled back into also from a part for the effluent of the second methanator
Into the feeding flow of the first reactor.This recycling can be by driven compressor, or can be driven by injector.
In the previous application (WO2012/084076) of the applicant, find by carefully analyzing thermokinetics and reaction
Condition can be controlled by temperature and determine optimum operation window with the combination of steam addition.It has also been found that there are C2+ hydrocarbon
In the case of, using injector come drive the recycling of product gas be it is particularly advantageous that because by injector increase steam add
The effect added will have the function of increasing recycling, and the combination increase of steam addition and recycling will reduce carbonaceous material
There is synergistic effect in terms of formation.
In the previous application, action pane is by by making feed gas balance obtain according to methanation reaction
Operation temperature T and methanation balanced gas with unconverted higher hydrocarbon steam and advanced hydrocarbon molecule in carbon ratio
What S/HHC was limited.In widest form, the action pane for methanation cover at least 1% C2+ hydrocarbon presence
Under, at a temperature of higher than 460 DEG C, under the S/HHC ratios less than 25 and in the temperature less than T=(30S/HHC+425) DEG C
Operation under degree.
If reaction is exothermic, during by catalyst bed in adiabatic reactor, reactants and products
Temperature can increase.On the other hand, this raised temperature tends to that balance is made to move towards lower methane concentration.Therefore,
Only by keeping reaction gas cold in a manner of such or is such (such as by making to be recycled through cooling product gas)
But carry out limit temperature raising, could complete or be nearly completed, such as US 4, disclosed in 130,575.
It is well known that the temperature of methanation reaction can be controlled by adding steam into synthesis gas, such as apply for EP 2
Disclosed in 110 425.This steam addition includes especially higher hydrocarbon (C in charging>1) in the case of, have and reduce whisker
The effect that carbon (otherwise it may be damaged catalyst) is formed.
Therefore, the present invention relates to one kind for from from coke oven, gasification from coal, biomass and/or waste or is originated from
The method of product gas of the synthesis gas of the biogas or pyrolysis gas charging production rich in methane, the method includes
(a) will come from the first methanator and, if applicable, also from the stream of the second methanator
It includes injector to go out the feeding flow that the part of object is recycled back into the first reactor, which is configured as
With steam feed as power gas (motive gas) and with the product gas rich in methane recycled as drive
It takes offence body, the steam generates in the boiling-water reactor or boiler in the first methanator downstream；
(b) injector is run with superheated steam；
(c) liquid water is removed in throttle valve downstream；
(d) steam from dry drum (steam drum) is divided into recirculation flow and stream to be output；With
(e) using at least part of isenthalpic throttling of the steam from dry drum, then in throttle valve upstream by steam
It is reheated with its own, (process-fired) superheater without technique heating.
Steam with its own reheat and means that the steam reheats respectively with the steam from dry drum.
The superheater of technique heating is the superheater that (fired) is heated by process heat.If heated using technique
Superheater, such as in dry drum or be connected to dry drum.
By a part for the effluent from the first methanator be recycled back into first reactor into
Stream includes injector, which is configured with steam feed and is rich in first as power gas and with recycling
The product gas of alkane is as driving gas, and associated benefits are, provide recycling, without any energy for pumping
Amount, also need not be with the pump of movable part.Particularly, it is to have suction by the use for adding the recycling of steam via injector
Gravitation, because steam can be used to drive injector so that product stream recycles, without additional energy expenditure.Cause
This, the use of injector allows to be combined adjusting to the steam content in temperature and charging, and to work as, there are advanced in raw material
When hydrocarbon, it is no more than the critical combinations of operation temperature and the critical ratio of steam and higher hydrocarbon.
The design of injector for being operated under high temperature and pressure and different capabilities is comparatively simple, and this injector phase
To cheap.Therefore, other than improving energy economy, the use of injector additionally aids the whole warp for improving methanation process
Ji property.
However, being clearly best with superheated steam operation injector, because saturated vapor may cause etching problem；And
And the device based on boiling-water reactor (BWR) usually only generates saturated vapor, adds because can not possibly generate technique in SNG units
The overheat of heat.The problem of this is injector.
It has now surprisingly been found that this problem can by the so-called isenthalpic throttling of the steam from dry drum,
Then steam is reheated " with its own " to solve, the fact that constitute the present invention key.
Constant-enthalpy process (isenthalpic process or isoenthalpic process) be defined as in no enthalpy or
The process carried out in the case of any variation of specific enthalpy.
During stable state, current stabilization, the significant changes of pressure and temperature may occur for fluid, but if not arriving surrounding
Environment or the heat transmitted from ambient enviroment, do not do work to ambient enviroment or by ambient enviroment, and do not have fluid dynamic energy
Change, then the process is still constant enthalpy.
Throttling process is the good example of constant-enthalpy process.It is let out if we consider that promoting (lifting) on pressure vessel
Pressure valve or safety valve, the then specific enthalpy when specific enthalpy of the fluid in pressure vessel is escaped with fluid from valve are identical.It is flowed by understanding
The specific enthalpy and the pressure outside pressure vessel of body, it may be determined that escape the temperature and speed of fluid.
The invention also includes apparatus for carrying out the method, the equipment includes：
First methanator of boiling-water reactor form, the front can have sulphur protection；It is adiabatic with optional second
Methanator；And further include
Superheater；
Dry drum；
Knockout drum (knock out drum)；With
Injector,
Isenthalpic throttling wherein is carried out at least part of the steam from dry drum, then in throttle valve upstream by steam
It is reheated with its own, thus generates the superheated steam needed for operation injector.
Knockout drum is a kind of vapour-liquid separator, for detaching vapour-liquid mixing usually in several commercial Applications
Object.
In the method for the invention, preferably 30 bars high about 85 bars higher than the operation pressure in reactor, it is most preferably high by 40
Bar pressure under generate saturated vapor.Preferably by using dedicated heat exchanger or by that will restrain or coil is inserted into steaming
Overheat is realized in steam drum.
The present invention is explained further with reference to figure 1-6.Wherein, Fig. 1-4 and Fig. 6 is shown according to the present invention for passing through
The possibility mode of arrangement heating and injector, Fig. 5 are shown with biography in the equipment for the product gas that method production is rich in methane
The Known designs of the superheater of system heating.
More specifically, Fig. 1 shows a possible embodiment of the equipment of the present invention, wherein with boiling water (102)
Some steam (116) generated in the dry drum of charging the gas of heating from knockout drum (140) in heat exchanger (120)
Phase (144), and remaining steam (124) generated in dry drum is exported.By through cooling steam (122) via valve (130)
It is fed to the knockout drum (140).Boiling water (112) from dry drum is fed to methanator and via pipeline
(104) dry drum is returned to.Heated gas phase (146) is for feeding to injector.
Although the embodiment functions satisfactorily, it has the shortcomings that small, i.e., must periodically clean valve (130).
Fig. 2 shows another embodiments of the equipment of the present invention, wherein positioned at the dry drum fed with boiling water (202)
(210) gas phase (244) of heater (220) heating from knockout drum (240) in.It will be through cooling steam (222) portion
Divide ground to be fed to the knockout drum (240) via valve (230), and is partly exported via pipeline (224).Heated
Gas phase (246) is for feeding to injector.
In the another embodiment of the equipment according to the present invention shown in Fig. 3, heat exchanger (320) with in Fig. 1
Roughly the same mode is located at outside dry drum, but the one of the interior steam generated of the dry drum (310) for specifically using boiling water (302) to feed
Partly (315) then send back to dry drum by heat exchanger (320) via pipeline (322).In this way, the steaming from dry drum
Vapour is reheated " with its own ", while by heated gas phase (346) for feeding to injector.
Fig. 4 shows the more complete device layout of the present invention comprising the dry drum of Fig. 1/knockout drum setting, but
Further include boiling water methanator (460) and injector (450), which is configured with steam feed work
For power gas and the product gas rich in methane with recycling is as driving gas.More specifically, injector (450)
The steam (464) of origin automatic heat-exchanger (420) and the effluent rich in methane also from methanator (460)
(462) a part (466) is fed.
Fig. 5 shows the superheater design of the traditional heating for methanation equipment, and the design includes methanation reaction
Device (570), heater (560), heat exchanger (520) and injector (550), injector (550) the origin automatic heat-exchanger
(520) it gas (522) and is fed also from a part (566) for the effluent (564) of methanator.
Finally, Fig. 6 shows the more complete device layout of the present invention comprising dry drum/knockout drum of Fig. 2,
But further include boiling water methanator (670) and injector (650), which is configured with steam feed
As power gas and the product gas rich in methane with recycling is as driving gas.More specifically, injector
(650) by coming from the steam (664) for the heater being located in dry drum (610) and also from methanator (670)
The part (666) of the effluent (672) rich in methane fed.
The following table shows the Known designs of the superheater with traditional heating (Fig. 5) and according to the present invention newly-designed two
A embodiment (Fig. 4, isothermal；And Fig. 6, it is adiabatic) between comparison.
*) according to the present invention
Although can be seen that compared with the control, power steam has lower temperature, the method or defeated of the present invention
More steam are gone out, this is because the pressure drop in recirculation circuit is relatively low, this is based on the fact that：Not according to the present invention
There are process steam superheaters.
The inventive process provides the alternative solutions of process steam superheater.It is particularly useful to small decorative device.
In addition, this method compensates for the shortage of the process heat for overheat in the BWR devices based on injector, and it can be exported
Both superheated steams of high and medium voltage.
Claims (5)
1. one kind is for from the gasification for from coke oven, being originated from coal, biomass and/or waste or from biogas or pyrolysis gas
The method of product gas of the synthesis gas charging production rich in methane, the method includes
(a) will come from the first methanator and, if applicable, also from the effluent of the second methanator
A part to be recycled back into the feeding flow into the first reactor include injector, the injector is configured as having
There is steam feed as power gas and the product gas rich in methane with recycling is as driving gas, the steam
It is generated in the boiling-water reactor or boiler in the first methanator downstream；
(b) injector is run with superheated steam；
(c) liquid water is removed in throttle valve downstream；
(d) steam from dry drum is divided into recirculation flow and stream to be output；With
(e) using at least part of isenthalpic throttling of the steam from dry drum, steam is then used it in throttle valve upstream
Itself is reheated, without the superheater of technique heating, i.e., the superheater heated by process heat.
2. preferably high by 30 according to the method described in claim 1, wherein about 85 bars higher than the operation pressure in the reactor
Bar, generate saturated vapor under most preferably high 40 bars of pressure.
3. method according to claim 1 or 2, wherein realizing overheat by using dedicated heat exchanger.
4. method according to claim 1 or 2, wherein being realized by that will restrain or coil be inserted into dry drum
Heat.
5. a kind of for implementing equipment method according to claim 1 to 4, the equipment includes：
First methanator of boiling-water reactor form, the front can have sulphur protection；With the optional second adiabatic methane
Change reactor；And further include
Superheater；
Dry drum；
Knockout drum；With
Injector,
Isenthalpic throttling wherein is carried out at least part of the steam from dry drum, steam is then used it in throttle valve upstream
Itself is reheated, and the superheated steam needed for operation injector is thus generated.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DKPA201600156 | 2016-03-14 | ||
| DKPA201600156 | 2016-03-14 | ||
| PCT/EP2017/055274 WO2017157720A1 (en) | 2016-03-14 | 2017-03-07 | Process and apparatus for the production of methanated gas |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN108779405A true CN108779405A (en) | 2018-11-09 |
| CN108779405B CN108779405B (en) | 2020-11-24 |
Family
ID=58231633
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201780017030.5A Active CN108779405B (en) | 2016-03-14 | 2017-03-07 | Method and plant for producing a methanated gas |
Country Status (5)
| Country | Link |
|---|---|
| CN (1) | CN108779405B (en) |
| FI (1) | FI129276B (en) |
| RU (1) | RU2018136053A (en) |
| SE (1) | SE544691C2 (en) |
| WO (1) | WO2017157720A1 (en) |
Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE19538674A1 (en) * | 1995-10-17 | 1997-04-24 | Siemens Ag | Process and device for generating superheated steam from saturated steam and steam power plant |
| US7442233B2 (en) * | 2005-07-06 | 2008-10-28 | Basf Catalysts Llc | Integrated heavy hydrocarbon removal, amine treating and dehydration |
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| DE3032123A1 (en) * | 1979-10-22 | 1981-04-30 | Conoco Inc., 74601 Ponca City, Okla. | METHOD FOR PRODUCING A METHANE-REPLACING NATURAL GAS |
| RU2073172C1 (en) * | 1994-07-27 | 1997-02-10 | Казанский государственный технический университет им.А.Н.Туполева | Method and device for generation of superheated steam at constant temperature |
| CN102482174B (en) * | 2009-08-03 | 2014-09-10 | 国际壳牌研究有限公司 | Process for the co-production of superheated steam and methane |
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2017
- 2017-03-07 WO PCT/EP2017/055274 patent/WO2017157720A1/en active Application Filing
- 2017-03-07 RU RU2018136053A patent/RU2018136053A/en not_active Application Discontinuation
- 2017-03-07 FI FI20185711A patent/FI129276B/en active IP Right Grant
- 2017-03-07 CN CN201780017030.5A patent/CN108779405B/en active Active
- 2017-03-07 SE SE1851239A patent/SE544691C2/en unknown
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| DE19538674A1 (en) * | 1995-10-17 | 1997-04-24 | Siemens Ag | Process and device for generating superheated steam from saturated steam and steam power plant |
| US7442233B2 (en) * | 2005-07-06 | 2008-10-28 | Basf Catalysts Llc | Integrated heavy hydrocarbon removal, amine treating and dehydration |
| CN101338231A (en) * | 2006-05-03 | 2009-01-07 | 深圳市星原燃气轮机维修开发有限公司 | Natural gas or hydrogen gas made from coal |
| CN102421506A (en) * | 2009-03-31 | 2012-04-18 | 罗米克控股有限公司 | Method for separating a medium mixture into fractions |
| CN103080049A (en) * | 2010-07-28 | 2013-05-01 | 蒂森克虏伯伍德有限公司 | Process for producing a methane-containing gas from synthesis gas and methane production plant for carrying out the process |
| CN103119137A (en) * | 2010-07-29 | 2013-05-22 | 鲁奇有限责任公司 | Method for producing substitute natural gas |
| WO2012084076A1 (en) * | 2010-12-20 | 2012-06-28 | Haldor Topsøe A/S | Process for the production of methane rich gas |
| DE102012218526A1 (en) * | 2012-10-11 | 2014-04-17 | Zentrum für Sonnenenergie- und Wasserstoff-Forschung Baden-Württemberg | Method and device for producing a methane-containing natural gas substitute and associated energy supply system |
Also Published As
| Publication number | Publication date |
|---|---|
| SE544691C2 (en) | 2022-10-18 |
| FI129276B (en) | 2021-11-15 |
| RU2018136053A3 (en) | 2020-07-03 |
| FI20185711A (en) | 2018-08-29 |
| RU2018136053A (en) | 2020-04-15 |
| WO2017157720A1 (en) | 2017-09-21 |
| CN108779405B (en) | 2020-11-24 |
| SE1851239A1 (en) | 2018-10-10 |
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